CN102247740A - Multi-stage desorption process for desulfurization solution - Google Patents
Multi-stage desorption process for desulfurization solution Download PDFInfo
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- CN102247740A CN102247740A CN2011102074646A CN201110207464A CN102247740A CN 102247740 A CN102247740 A CN 102247740A CN 2011102074646 A CN2011102074646 A CN 2011102074646A CN 201110207464 A CN201110207464 A CN 201110207464A CN 102247740 A CN102247740 A CN 102247740A
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Abstract
The invention provides a multi-stage desorption process for desulfurization solution. The process comprises the following steps of: desorbing rich liquor of first desulfurization solution at a first desorption section to obtain semi-lean solution of the desulfurization solution and desorbed gas; and desorbing rich liquor of second desulfurization solution at a second desorption section to obtain lean solution of the desulfurization solution and desorbed gas, wherein the content of sulfur oxide in the rich liquor of the first desulfurization solution is higher than the content of sulfur oxide in the rich liquor of the second desulfurization solution, and the content of sulfur oxide in the semi-lean solution is higher than the content of sulfur oxide in the lean solution.
Description
Technical field
The present invention relates to remove the technical field of sulfur in smoke, the multistage desorption technique of particularly a kind of desulfuration solution.
Background technology
In a kind of existing flue gas desulfurization technique, utilize amine liquid to absorb sulfur in smoke, and in the high temperature desorption process, the amine liquid that has absorbed sulfur dioxide is carried out desorb, obtain the sulfur dioxide gas of higher degree, and making amine liquid recover to absorb the ability of sulfur dioxide in flue gas, amine liquid can recycle.
At present, also have a kind of process of renewable ionic liquid desulfurization, the process of this technology is similar substantially to the process of above-mentioned amine method sulfur removal technology.Both differences are desulfurization absorption liquid component difference, and it absorbs the ability basically identical of sulfur dioxide.Renewable ionic liquid sulfur removal technology generally includes one-level and absorbs and one-level desorb (desorb is promptly regenerated), and under the big situation of dust content, adopts flue gas prewashing technology.
In existing desulfuration solution desorption technique, there is the big problem of desorb energy consumption.Specifically, rich solution is when just beginning desorb, and desorption rate is fast, and the desorb energy consumption is little, along with the further reduction of desulfuration solution sulphur oxide content, separates the identical many oxysulfide gas of sucking-off, and needed desorb energy consumption increases greatly.In addition, desorb flue gas condensing water directly returns desorption system, and condensed water directly influences the desorption efficiency and the desorb energy consumption of desulfurization rich solution.
Summary of the invention
The object of the present invention is to provide the multistage desorption technique of desulfuration solution of at least one technical problem in a kind of can the solving the problems of the technologies described above.
The multistage desorption technique of desulfuration solution according to the present invention may further comprise the steps: at first stripping stage first desulfuration solution rich solution is carried out desorb, obtain desulfuration solution semi lean solution and desorption gas; At second stripping stage second desulfuration solution rich solution is carried out desorb, obtain desulfuration solution lean solution and desorption gas, wherein, the oxysulfide content of the first desulfuration solution rich solution is higher than the oxysulfide content of the second desulfuration solution rich solution, and the oxysulfide content of semi lean solution is higher than the oxysulfide content of lean solution.
This technology also can be included in second stripping stage part of desulfuration solution semi lean solution is carried out desorb, and the remainder of desulfuration solution semi lean solution can be used as the desulfuration solution that absorbs sulfur dioxide gas.
The first desulfuration solution rich solution is contacted with desorption gas from second stripping stage, make the desulfuration solution rich solution of winning form desulfuration solution semi lean solution and desorption gas.
The second desulfuration solution rich solution is contacted with the heat steam of desulfuration solution lean solution, make the second desulfuration solution rich solution form desulfuration solution lean solution and desorption gas.
The described part of the second desulfuration solution rich solution and desulfuration solution semi lean solution is contacted with the heat steam of desulfuration solution lean solution, make the described part of the second desulfuration solution rich solution and semi lean solution form desulfuration solution lean solution and desorption gas.
This technology also can comprise to be handled desorption gas.
The step that desorption gas is handled can comprise condensation, gas-liquid separation and sulfur filtration.
The step of condensation can comprise carries out one-level condensation and B-grade condensation successively to desorption gas.
In the one-level condensation process, can make the first desulfuration solution rich solution and desorption gas carry out heat exchange, make the first desulfuration solution rich solution enter first stripping stage then from absorption system.
In the B-grade condensation process, can carry out condensation to desorption gas; Can obtain gas-liquid mixture to condensation and carry out gas-liquid separation, isolated gas can be delivered to acid making system, can carry out sulfur filtration isolated liquid; Can obtain condensate liquid to condensation and carry out sulfur filtration.
The condensate liquid and the described isolated liquid that carry out obtaining after the sulfur filtration can be sent into first stripping stage.
Description of drawings
The detailed description that the present invention is carried out in conjunction with the drawings, characteristics of the present invention will become clearer and be easy to and be understood, in the accompanying drawings:
Fig. 1 is the schematic diagram that shows according to the renewable flue gas desulphurization system of exemplary embodiment of the present invention;
Fig. 2 is the schematic diagram that shows the multistage desorption system of desulfuration solution in the renewable according to an exemplary embodiment of the present invention flue gas desulphurization system and use the multistage desorption technique of desulfuration solution of the multistage desorption system realization of this desulfuration solution.
Main Reference numeral:
100: absorption system
110: semi lean solution absorber portion 111: 113: the first flue gases of semi lean solution inlet rich solution outlet in 112: the first rise 116: the first base plates of gas hood 115: the first liquid distribution troughs of 114: the first packing layers
120: lean solution absorber portion 121: 123: the second flue gases of lean solution inlet rich solution outlet in 122: the second rise 126: the second base plates of gas hood 125: the second liquid distribution troughs of 124: the second packing layers
130: desulfuration solution captures section 131: cleaning solution inlet 132: 133: the three flue gases of trapping solution outlet rise 136: the three base plates 137 of gas hood 135: the three liquid distribution troughs of 134: the three packing layers: capture the section circulating pump
140: the demist section
200: desorption system
211: the first rich solution inlets 212 of 210: the first stripping stages: 216: the first base plates of semi lean solution 213: the first liters of gas hood 215: the first spray throwers of 214: the second packing layers of outlet
221: the second rich solution inlets 222 of 220: the second stripping stages: 226: the second base plates of lean solution 223: the second liters of gas hood 225: the second spray throwers of 224: the three packing layers of outlet
230: reboiler
240: the first packing layers
300: desulfuration solution cleaning system 310: sedimentation filtration system 320: freezing and crystallizing system 311: settler 312: filter
330: the resin desalination system
430: the three pipelines of 420: the second pipelines of 410: the first pipelines
413: the second poor rich liquid heat exchangers of 412: the first poor rich liquid heat exchangers
500: the flue gas washing system
600: the desorption gas treatment system
The specific embodiment
Now, will describe exemplary embodiment of the present invention in detail, example of the present invention illustrates in the accompanying drawings, and wherein, identical label is represented components identical all the time.To embodiment be described by the reference accompanying drawing below, to explain the present invention.Yet the present invention can implement with multiple different form, should not be understood that to be confined to the exemplary embodiment in this proposition.It openly will be thorough with completely providing these embodiment to make of the present invention, and scope of the present invention is conveyed to those skilled in the art fully.In the accompanying drawings, for clarity, can exaggerate the layer and the zone size and relative size.
But usage space relative terms here, as " following ", " in ... below ", " top " etc., be used for describing like a cork as shown in FIG. element or the relation of feature and other element or feature.It should be understood that the space relative terms is intended to comprise the different azimuth of device in using or operating except the orientation that is described in the drawings.For example, if device is reversed in the accompanying drawings, then be described as other element or feature " following " or " " element of other element or feature " below " will be positioned as subsequently other element or feature " above " or " " element or the feature of other element or feature " top ".Therefore, exemplary term " following " can comprise top and following two kinds of orientation.Described device can correspondingly be explained space used herein relative descriptors by other location (revolve turn 90 degrees or in other orientation).
In order to understand the present invention better, before embodiment was described in detail, employed part term was simply explained in need describing the present invention.In this manual, sulfur-containing smoke gas to be desulfurization (hereafter is a flue gas) can comprise at least a in sinter fume, metallurgical gas, the flue gas in power station boiler etc., and oxysulfide wherein mainly is a sulfur dioxide; But sulfur-containing smoke gas to be desulfurization is not limited thereto.In this specification, " desulfuration solution " is meant the solution of the oxysulfide that is used for removing flue gas, " desulfuration solution rich solution " (below abbreviate " rich solution " as) referred to absorb the desulfuration solution of sulfur dioxide, " desulfuration solution lean solution " (below abbreviate " lean solution " as) is meant the desulfuration solution that does not absorb sulfur dioxide or separated sucking-off the desulfuration solution of the sulfur dioxide that is absorbed, wherein, if desulfuration solution is deviate from the sulfur dioxide of absorption by twice above desorb, then after desorb desulfurization first and the last time the desulfuration solution before the desorb desulfurization can be called " desulfuration solution semi lean solution " (below abbreviate " semi lean solution " as), and the desulfuration solution after the last desorb desulfurization is " lean solution "; If the desulfuration solution rich solution is only deviate from the sulfur dioxide that is absorbed by a desorb, the desulfuration solution after the desorb desulfurization just can be described as " lean solution " so.Therefore, the oxysulfide content of semi lean solution is higher than the oxysulfide content of lean solution, i.e. the ability that the energy force rate semi lean solution of lean solution absorption oxysulfide absorbs oxysulfide is strong.
In this manual, the main absorbent components in the desulfuration solution promptly can absorb oxysulfide and can make the composition of oxysulfide desorb, can comprise at least a in amine liquid and the ionic liquid.In addition, desulfuration solution also comprises activator, acid and water.Selectively, desulfuration solution also comprises surfactant.Yet, the invention is not restricted to this.
Describe renewable according to an exemplary embodiment of the present invention flue gas desulphurization system, the multistage desorption system of desulfuration solution wherein and and the multistage desorption technique of desulfuration solution realized by the multistage desorption system of this desulfuration solution below with reference to accompanying drawings in detail.
Fig. 1 is the schematic diagram that shows according to the renewable flue gas desulphurization system of exemplary embodiment of the present invention.
Illustrate as Fig. 1, renewable according to an exemplary embodiment of the present invention flue gas desulphurization system comprises: absorption system 100 absorbs sulfur in smoke by lean solution is contacted with pending flue gas adverse current, and forms rich solution and Purge gas; Desorption system 200 is by utilizing reboiler heating rich solution and making rich solution carry out desorb in desorber, to form new lean solution (will be recycled) and desorption gas; Desulfuration solution cleaning system 300 comprises sedimentation filtration system 310, freezing and crystallizing system 320 and resin desalination system 330, with suspension, metal cation and the foreign ion equity in the lean solution after the removal desorb; Washing system 500 is arranged on before the absorption system 100, is used to wash the flue gas that contains oxysulfide that is about to enter absorption system 100, to remove the impurity such as dust that contain in the flue gas; Desorption gas treatment system 600 utilizes condensation separator to make to separate the sulfur dioxide gas of sucking-off to separate with the desulfuration solution of carrying secretly, to obtain pure sulfur dioxide gas and to reclaim condensed fluid simultaneously.Desorption gas treatment system 600 also can be included in the desorption system 200, because desorption gas treatment system 600 plays the effect that sulfur dioxide gas is separated with desulfuration solution, promptly further deviates from sulfur dioxide gas from desulfuration solution.
Fig. 2 is the schematic diagram that shows the multistage desorption system of desulfuration solution in the renewable according to an exemplary embodiment of the present invention flue gas desulphurization system and use the multistage desorption technique of desulfuration solution of the multistage desorption system realization of this desulfuration solution.Hereinafter, describe the multistage desorption system 200 of desulfuration solution in detail with reference to Fig. 2.
As Fig. 2 and shown in Figure 1, the multistage desorption system 200 of desulfuration solution comprises first stripping stage 210 and second stripping stage 220 that sets gradually along the desulfuration solution flow direction according to an exemplary embodiment of the present invention.210 pairs of desulfuration solutions of first stripping stage (that is, rich solution) carry out elementary desorb, and the semi lean solution of separating sucking-off is admitted to second stripping stage 220 and carries out degree of depth desorb.The desorption gas that desulfuration solution obtains after first stripping stage 210 and 220 desorbs of second stripping stage passes through condenser 610 and gas-liquid separator 620 successively, thereby the sulfur dioxide gas that obtains is sent into the acid making system (not shown).
Specifically, the multistage desorption system 200 of desulfuration solution comprises housing 201, is arranged on first packing layer 240, second packing layer 214 and the 3rd packing layer 224 in the housing 201 from top to bottom according to an exemplary embodiment of the present invention.First spray thrower 215 and first liquid distribution trough 217 are successively set between first packing layer 240 and second packing layer 214.First liter of gas hood 213, first base plate 216, second spray thrower 225, second liquid distribution trough 227 are successively set between second packing layer 214 and the 3rd packing layer 224.The second liter of gas hood 223 and second base plate 226 are arranged on the 3rd packing layer 224 belows,, are arranged on the bottom of housing 201 that is.The effect of spray thrower is even spraying liquid, and liquid distribution trough distributes the liquid that is sprayed by spray thrower equably to the packing layer of correspondence.The effect that rises gas hood and base plate is that desorption gas is evenly risen.
The sidewall of housing 201 and place, top are provided with a plurality of entrance and exits of desulfuration solution and desorption gas respectively.Housing 201 can be cylindrical vessel, but the invention is not restricted to this.
To describe first stripping stage 210 below in detail according to the multistage desorption system 200 of the desulfuration solution of the embodiment of the invention.
First rich solution inlet 211 is arranged on the sidewall on housing 201 tops, and the rich solution of discharging from absorption system 100 (see figure 1)s enters housing 201 from first rich solution inlet 211 after heat exchange.Specifically, first rich solution inlet 211 links to each other with first spray thrower 215, thereby the rich solution from absorption system 100 enters housing 201 through first rich solution inlet 211, be sprayed on first liquid distribution trough 217 by first spray thrower 215, the liquid after 217 pairs of rich solutions of first liquid distribution trough distribute and will distribute is transported to second packing layer 214.
Semi lean solution outlet 212 is arranged on the sidewall at housing 201 middle parts.The part of the semi lean solution that obtains after 210 desorbs of first stripping stage is discharged from semi lean solution outlet 212, is supplied to semi lean solution absorber portion 110 (see figure 1)s of absorption system 100 after 413 heat exchange of second poor rich liquid heat exchanger along first pipeline 410.Alternatively, on first pipeline 410, between second poor rich liquid heat exchanger 413 and semi lean solution absorber portion 110, also be provided with semi lean solution filter (not shown among Fig. 2).
In addition, be provided with desorption gas treatment system 600 above first stripping stage 210, desorption gas treatment system 600 comprises condenser 610, gas-liquid separator 620 and sulfur filtration device 630.Condenser 610 comprises first-stage condenser 610-1 and secondary condenser 610-2.
That is to say, the rich solution that comes out from the bottom of absorption system 100 (for example about 48 ℃) enters rich solution groove (not shown) and cushions, then after suspension filters, squeeze into poor rich liquid heat exchanger 413 through rich solution pump (not shown) and be warming up to for example about 85 ℃, enter first-stage condenser 610-1, for example about 115 ℃ high temperature desorption gas by the discharging of first stripping stage 210 is heated to for example about 95 ℃, enters desorption system 200 from the top of classification desorption system 200 and carries out desorb.Alternatively, a part of desulfuration solution is heated to for example about 120 ℃ through reboiler 230 and carries out desorb.
For example about 115 ℃ steam and the sulfur dioxide gas that come out from the top of first stripping stage 210, after first-stage condenser 610-1 and rich solution carry out heat exchange, adopt secondary condenser 610-2 heat exchange again, therefore, most of steam is condensed and temperature is reduced to for example about 95 ℃ at first-stage condenser 610-1, and gas enters secondary condenser 610-2, continue to be cooled to for example about 40～60 ℃ after gas-liquid separator 620 separates, sulfur dioxide gas is regulated through pressure, delivers to acid making system.
To describe second stripping stage 220 below in detail according to the multistage desorption system 200 of the desulfuration solution of the embodiment of the invention.
Second rich solution inlet 221 is arranged on the sidewall at housing 201 middle parts.Part from the rich solution of absorption system 100 can directly enter the multistage desorption system 200 of desulfuration solution through second rich solution inlet 221 after 412 heat exchange of first heat exchanger, and carries out heat exchange without second heat exchanger 413.
Second rich solution inlet 221 is connected with second spray thrower 225, therefore, the rich solution that directly enters second rich solution inlet 221 after 412 heat exchange of first heat exchanger from absorption system 100 is distributed to the 3rd packing layer 224 equably again by second spray thrower 225 and second liquid distribution trough 227.The rich solution that enters thus carries out desorb at second stripping stage 220.Selectively, the rich solution that enters thus carries out desorb with the semi lean solution from first stripping stage 210 at second stripping stage 220.The semi lean solution that the 3rd packing layer 224 portion from it of prolonging enters and the fall time of rich solution, thus make semi lean solution and rich solution carry out abundant desorb, to improve desorption efficiency.In addition, the gas that the 3rd packing layer 224 produces rich solution and semi lean solution and reboiler 230 (will be explained hereinafter) carries out counter current contacting, so that rich solution and semi lean solution are heated, thereby improves desorption efficiency.
In addition, at second stripping stage 220, be provided with reboiler 230.Reboiler 230 is connected with housing 201 by reboiler inlet 229 and reboiler outlet 229 '.Specifically, reboiler inlet 229 is arranged on the sidewall of housing 201 bottoms and is positioned at second base plate, 226 tops, and reboiler outlet 229 ' is arranged on the sidewall of housing 201 bottoms and is positioned at second base plate, 226 belows.Reboiler 230 will be separated the desulfuration solution (that is, semi lean solution) of sucking-off part sulfur dioxide gas and be heated into gas from the rich solution of absorption system 100, deliver to second base plate, 226 belows through reboiler outlet 229 ' then.The gas that produces from reboiler 230 enters the 3rd packing layer 224 through second base plate 226 and second liter of gas hood 223, and carries out heat exchange with rich solution and semi lean solution in the 3rd packing layer 214, with further raising desorption efficiency.
Therefore, in the multistage desorption technique of multistage desorption system of desulfuration solution according to the present invention and the multistage desorption system realization of employing, the semi lean solution of segmentation desorb and lean solution enter the different absorber portion of absorption system respectively, need not to the desulfuration solution rich solution carry out completely, disposable desorb, therefore reduce desulfuration solution desorb degree, reduced desulfuration solution desorb energy consumption.
In addition, in first stripping stage of the multistage desorption system of desulfuration solution according to the present invention, utilize desorption gas and rich solution to carry out heat exchange, utilized system energy consumption fully, reduced the heating energy consumption.
In addition, desorb flue gas condensing water does not directly return the stripping stage of desorption system, thereby can not influence the desorption efficiency and the desorb energy consumption of desulfurization rich solution.
Although describe and show the present invention, under the situation of the scope and spirit that do not break away from the application who is defined by the claims, can make various modification in form and details in conjunction with exemplary embodiment of the present invention.
Claims (12)
1. multistage desorption technique of desulfuration solution is characterized in that may further comprise the steps:
At first stripping stage first desulfuration solution rich solution is carried out desorb, obtain desulfuration solution semi lean solution and desorption gas;
At second stripping stage second desulfuration solution rich solution is carried out desorb, obtains desulfuration solution lean solution and desorption gas,
Wherein, the oxysulfide content of the first desulfuration solution rich solution is higher than the oxysulfide content of the second desulfuration solution rich solution, and the oxysulfide content of desulfuration solution semi lean solution is higher than the oxysulfide content of desulfuration solution lean solution.
2. the multistage desorption technique of desulfuration solution according to claim 1 is characterized in that described technology also comprises: at second stripping stage part of desulfuration solution semi lean solution is carried out desorb.
3. the multistage desorption technique of desulfuration solution according to claim 2, the remainder that it is characterized in that the desulfuration solution semi lean solution is as the desulfuration solution that absorbs sulfur dioxide gas.
4. the multistage desorption technique of desulfuration solution according to claim 1, it is characterized in that in first stripping stage, making the first desulfuration solution rich solution to contact, make the desulfuration solution rich solution of winning form desulfuration solution semi lean solution and desorption gas with desorption gas from second stripping stage.
5. the multistage desorption technique of desulfuration solution according to claim 1 is characterized in that making in second stripping stage second desulfuration solution rich solution to contact with the heat steam of desulfuration solution lean solution, makes the second desulfuration solution rich solution form desulfuration solution lean solution and desorption gas.
6. the multistage desorption technique of desulfuration solution according to claim 2, it is characterized in that in second stripping stage, making the described part of the second desulfuration solution rich solution and desulfuration solution semi lean solution to contact, make the described part of the second desulfuration solution rich solution and desulfuration solution semi lean solution form desulfuration solution lean solution and desorption gas with the heat steam of desulfuration solution lean solution.
7. the multistage desorption technique of desulfuration solution according to claim 1 is characterized in that described technology also comprises desorption gas is handled.
8. the multistage desorption technique of desulfuration solution according to claim 7 is characterized in that the step that desorption gas is handled is comprised condensation, gas-liquid separation and sulfur filtration.
9. the multistage desorption technique of desulfuration solution according to claim 8, the step that it is characterized in that condensation comprises carries out one-level condensation and B-grade condensation successively to desorption gas.
10. the multistage desorption technique of desulfuration solution according to claim 9 is characterized in that making in the one-level condensation process the first desulfuration solution rich solution and desorption gas from absorption system to carry out heat exchange, makes the first desulfuration solution rich solution enter first stripping stage then.
11. the multistage desorption technique of desulfuration solution according to claim 9 is characterized in that in the B-grade condensation process desorption gas being carried out condensation; Condensation is obtained gas-liquid mixture carry out gas-liquid separation, isolated gas is delivered to acid making system, isolated liquid is carried out sulfur filtration; Condensation is obtained condensate liquid carry out sulfur filtration.
12. the multistage desorption technique of desulfuration solution according to claim 11 is characterized in that condensate liquid and the described isolated liquid that will carry out obtaining after the sulfur filtration sends into first stripping stage.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104492243A (en) * | 2015-01-08 | 2015-04-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Flue gas desulphurization system and flue gas desulphurization process |
| CN105148667A (en) * | 2015-09-11 | 2015-12-16 | 永清环保股份有限公司 | High-efficiency desulfuration and dedusting system for flue gas purification |
| CN115228254A (en) * | 2022-07-12 | 2022-10-25 | 广东韶钢松山股份有限公司 | Desulfurization analysis system and switching method thereof |
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| CN1197763A (en) * | 1998-04-10 | 1998-11-04 | 刘金成 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
| CN201603504U (en) * | 2009-12-30 | 2010-10-13 | 中国恩菲工程技术有限公司 | Fume desulfurization system |
| CN201613102U (en) * | 2009-12-30 | 2010-10-27 | 中国恩菲工程技术有限公司 | Regeneration tower |
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- 2011-07-15 CN CN201110207464.6A patent/CN102247740B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1197763A (en) * | 1998-04-10 | 1998-11-04 | 刘金成 | Carbon dioxide eliminating technology used in ammonia synthesis and hydrogen production processes |
| CN201603504U (en) * | 2009-12-30 | 2010-10-13 | 中国恩菲工程技术有限公司 | Fume desulfurization system |
| CN201613102U (en) * | 2009-12-30 | 2010-10-27 | 中国恩菲工程技术有限公司 | Regeneration tower |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104492243A (en) * | 2015-01-08 | 2015-04-08 | 攀钢集团攀枝花钢铁研究院有限公司 | Flue gas desulphurization system and flue gas desulphurization process |
| CN105148667A (en) * | 2015-09-11 | 2015-12-16 | 永清环保股份有限公司 | High-efficiency desulfuration and dedusting system for flue gas purification |
| CN115228254A (en) * | 2022-07-12 | 2022-10-25 | 广东韶钢松山股份有限公司 | Desulfurization analysis system and switching method thereof |
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